CN220265583U - Promote lime production tail gas CO 2 Lime production system of concentration - Google Patents
Promote lime production tail gas CO 2 Lime production system of concentration Download PDFInfo
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- CN220265583U CN220265583U CN202321179395.7U CN202321179395U CN220265583U CN 220265583 U CN220265583 U CN 220265583U CN 202321179395 U CN202321179395 U CN 202321179395U CN 220265583 U CN220265583 U CN 220265583U
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- 235000008733 Citrus aurantifolia Nutrition 0.000 title claims abstract description 147
- 235000011941 Tilia x europaea Nutrition 0.000 title claims abstract description 147
- 239000004571 lime Substances 0.000 title claims abstract description 147
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 76
- 238000001816 cooling Methods 0.000 claims abstract description 85
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 81
- 239000003546 flue gas Substances 0.000 claims abstract description 79
- 239000007789 gas Substances 0.000 claims abstract description 73
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 66
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 66
- 239000001301 oxygen Substances 0.000 claims abstract description 66
- 238000001354 calcination Methods 0.000 claims abstract description 56
- 239000000446 fuel Substances 0.000 claims abstract description 44
- 239000007921 spray Substances 0.000 claims abstract description 9
- 239000000428 dust Substances 0.000 claims description 39
- 239000000779 smoke Substances 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 239000004744 fabric Substances 0.000 claims description 6
- 230000005540 biological transmission Effects 0.000 claims description 5
- 238000002485 combustion reaction Methods 0.000 abstract description 30
- 238000002156 mixing Methods 0.000 abstract description 18
- 239000012535 impurity Substances 0.000 abstract description 10
- 238000000034 method Methods 0.000 description 37
- 239000000047 product Substances 0.000 description 15
- 239000000463 material Substances 0.000 description 13
- 239000003245 coal Substances 0.000 description 7
- 235000019738 Limestone Nutrition 0.000 description 5
- 239000006028 limestone Substances 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- 239000012159 carrier gas Substances 0.000 description 3
- 239000002826 coolant Substances 0.000 description 3
- 239000000112 cooling gas Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- 238000005338 heat storage Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P40/00—Technologies relating to the processing of minerals
- Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills
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- Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
Abstract
Promote lime production tail gas CO 2 A concentrated lime production system comprising a lime kiln. The lime kiln is internally provided with a preheating section, a calcining section and a cooling section. The calcining section is internally provided with a fuel spray gun and is connected with a combustion-supporting air pipeline. The flue gas outlets of the calcining section and the cooling section are connected to the preheating section. The flue gas discharge pipeline led out from the flue gas outlet of the preheating section is divided into three branches, namely a fuel air conveying pipeline, a combustion-supporting flue gas pipeline and a heat exchange pipeline. Wherein the fuel delivery and supply air duct is connected to the fuel lance. The combustion-supporting flue gas pipeline is connected to a combustion-supporting air pipeline to assistThe air-fired pipeline is simultaneously connected with an oxygen conveying pipeline. The heat exchange pipeline is connected to the heat exchanger. The utility model changes the traditional air combustion supporting into O in the calcining section 2 With CO 2 Oxygen-enriched combustion-supporting of gas mixing, avoiding introducing N in fuel combustion process 2 CO of the impurity components 2 Greatly improves the tail gas CO in the lime production process 2 Concentration, high purity CO is obtained while lime is produced 2 And (3) gas.
Description
Technical Field
The utility model relates to a lime production system, in particular to a system for improving CO in tail gas of lime production 2 Concentration lime production system belongs to lime production facility technical field.
Background
Lime is an important industrial raw material and has wide application in the fields of metallurgy, construction and the like. The domestic lime yield in 2020 is about 3 hundred million tons, and the industrial scale is huge. At the same time, however, lime production results in large amounts of CO 2 And (5) discharging. Statistically, 1kg lime produced 1.1kg CO 2 Emission, so as to estimate the CO emitted to the atmosphere in the lime production process in China 2 The total amount exceeds 3 hundred million tons/year, and under the background of the carbon emission reduction and carbon peak reaching the full industry, the low CO is developed 2 The discharged lime production process and technology become hot spots and difficulties in technical research in the field.
The industrial lime production at the present stage mainly adopts a simple preheating-calcining-cooling process production technology. The heat required by the calcining step is provided by adopting a mode of directly supplying heat through fossil fuel combustion, the cooling step adopts normal-temperature air as a refrigerant medium, and the preheating step uses high-temperature flue gas generated by the calcining and cooling steps as a heat source. The process design can fully utilize the waste heat of the flue gas, and has higher fuel utilization efficiency. However, since the calcination flue gas is mixed with the cooling air, N in the tail gas 2 The impurity gases are more, so that CO in the exhaust gas is caused 2 The concentration is low, generally only (20-30%), so that CO in the tail gas is reduced 2 The difficulty of the enrichment and trapping technology is high, and the cost is high. Resulting in CO in tail gas of lime kiln at present 2 The enrichment and trapping are almost zero, and serious greenhouse gas emission and resource waste are generated。
Figure 2 is the most widely used lime production process at this stage. Lime raw material (limestone CaCO) at normal temperature (-20℃) 3 ) The material is gradually heated to a preheating temperature (about 600 ℃) in a preheating process, moisture (free or existing in the form of a compound) in the material is removed, and then the material enters a calcining process; in the calcination process, high-power heat is provided for the material, so that the material is quickly heated to about 1050 ℃, and the material is decomposed to generate CaO and release CO at high temperature 2 Completing calcination; the high temperature CaO produced is cooled to 100 ℃ in the cooling process to form the finished lime. The heat required by the material heating and material decomposition in the calcination process is usually provided by the combustion heat release of solid fuels such as raw coal, the cooling process adopts normal-temperature air as a cooling medium, high-temperature smoke generated in the cooling process and the calcination process enters the preheating process to provide heat for the material preheating, and finally low-temperature (120 ℃) tail gas is formed and is discharged from the system.
Under the above process, the combustion process of fossil fuel such as raw coal and the like and the air-based cooling process can introduce a large amount of N into the flue gas system 2 And the impurity components are such that CO in the tail gas of the exhaust system 2 The concentration is very low, typically only 20 to 30%. CO 2 Enrichment and trapping cost and CO in flue gas 2 Initial concentration is inversely related to CO 2 The lower the concentration, the higher the enrichment capture cost. Tail gas CO produced by lime in existing working procedure 2 Too low concentration results in high enrichment and trapping cost, which becomes a constraint for CO in the lime production process 2 The main obstacle for recycling.
Disclosure of Invention
Aiming at the tail gas CO produced by lime in the prior art 2 CO due to low concentration 2 The utility model provides a method for improving CO (carbon monoxide) in tail gas of lime production, which solves the problems of environmental pollution and resource waste caused by large emission amount and greenhouse gas emission 2 A lime production system of concentration. In the scheme of the utility model, the flue gas outlets of the calcination section and the cooling section of the lime kiln are connected to the preheating section, the flue gas discharge pipeline led out from the flue gas outlet of the preheating section is divided into three branches of a fuel air conveying pipeline, a combustion-supporting flue gas pipeline and a heat exchange pipeline,and the combustion-supporting air pipeline connected with the calcination section is respectively connected with the combustion-supporting flue gas pipeline and the oxygen conveying pipeline. Based on the structure of the device, the utility model changes the traditional air combustion-supporting air into O in the calcining section 2 With CO 2 Oxygen-enriched combustion-supporting air formed by mixing gas, thereby avoiding the introduction of N in the fuel combustion process in the prior art 2 CO of the impurity components 2 Greatly improves the tail gas CO in the lime production process 2 Concentration, i.e. high purity CO can be obtained while lime is being produced 2 Gaseous byproducts.
According to an embodiment of the utility model, a method for improving CO in tail gas of lime production is provided 2 A lime production system of concentration.
Promote lime production tail gas CO 2 A concentrated lime production system comprising a lime kiln. The lime kiln is internally provided with a preheating section, a calcining section and a cooling section. The calcining section is internally provided with a fuel spray gun and is connected with a combustion-supporting air pipeline. The flue gas outlets of the calcining section and the cooling section are connected to the preheating section. The flue gas discharge pipeline led out from the flue gas outlet of the preheating section is divided into three branches, namely a fuel air conveying pipeline, a combustion-supporting flue gas pipeline and a heat exchange pipeline. Wherein the fuel delivery and supply air duct is connected to the fuel lance. The combustion-supporting flue gas pipeline is connected to a combustion-supporting air pipeline, and an oxygen conveying pipeline is connected to the combustion-supporting air pipeline at the same time. The heat exchange pipeline is connected to the heat exchanger.
Preferably, the oxygen delivery pipeline is connected to the heat exchanger firstly, and the hot oxygen pipeline and the combustion-supporting flue gas pipeline led out from the outlet of the heat exchanger are connected to the combustion-supporting air pipeline after being combined.
In the utility model, a low-temperature hot air pipeline led out from the other outlet of the heat exchanger is divided into two branches, namely a cooling air pipeline and CO 2 And (5) a finished pipeline. Wherein the cooling air duct is connected to the cooling air inlet of the cooling section. CO 2 The finished pipeline is connected to CO 2 A finished product system.
Preferably, the cooling air duct is further provided with a cooler. Preferably, the cooler is a water bath or an air cooler.
Preferably, the system further comprises a mixer. The mixer is arranged at a position where the hot oxygen pipeline and the combustion-supporting flue gas pipeline are combined. The outlet of the mixer is connected with a combustion-supporting air pipeline.
In the present utility model, the system further comprises a first shunt. The first flow divider is arranged at the position of the smoke exhaust pipeline for separating three branches of the fuel delivery and air supply pipeline, the combustion-supporting smoke pipeline and the heat exchange pipeline.
In the present utility model, the system further comprises a second diverter. The second flow divider is arranged on the low-temperature hot air pipeline and is used for dividing a cooling air pipeline and CO 2 The positions of two branches of the finished pipeline.
In the present utility model, the system further comprises a dust remover. The dust remover is arranged on the flue gas discharge pipeline. Preferably, the dust remover is an electric dust remover or a cloth bag dust remover.
In the utility model, a first valve is arranged on the combustion-supporting flue gas pipeline. The oxygen transmission pipeline or the hot oxygen pipeline is provided with a second valve.
In the present utility model, the system further comprises a lime finishing system. And a discharge hole arranged at the bottom of the cooling section of the lime kiln is connected with a lime finished product system.
Aiming at tail gas CO produced by lime in the prior art 2 CO due to low concentration 2 The utility model provides a method for improving CO (carbon monoxide) in tail gas of lime production, which solves the problems of environmental pollution and resource waste caused by large emission amount and greenhouse gas emission 2 A lime production system of concentration. In the scheme of the utility model, the lime production system comprises a lime kiln, and a preheating section, a calcining section and a cooling section are arranged in the lime kiln. The calcining section is internally provided with a buried fuel spray gun (such as a pulverized coal spray gun), the calcining section is connected with a combustion-supporting air pipeline, and the upper part of the preheating section is provided with a flue gas outlet. The flue gas outlets of the calcining section and the cooling section are connected to the preheating section. The flue gas discharge pipeline led out from the flue gas outlet of the preheating section is divided into three branches, namely a fuel air conveying pipeline, a combustion-supporting flue gas pipeline and a heat exchange pipeline. Wherein the fuel delivery and supply air duct is connected to the fuel lance. The combustion-supporting flue gas pipeline is connected to a combustion-supporting air pipeline, and the combustion-supporting air pipeline is simultaneously connected with oxygen deliveryAnd (5) conveying the pipeline. The heat exchange pipeline is connected to the heat exchanger. Based on the structure of the device, the utility model changes the traditional air combustion-supporting air into oxygen and CO in the calcining section 2 Oxygen-enriched combustion-supporting air formed by mixing gas, thereby avoiding the introduction of N in the fuel combustion process in the prior art 2 CO of the impurity components 2 Is diluted to realize CO 2 The enrichment of the gas can thus be used for the calcination of the high-temperature flue gas (the main component is CO 2 Gas) to realize the CO required by the working procedures of carrier gas conveying, combustion air mixing, waste heat utilization and the like in the system 2 Self-circulation supply of gas, while producing lime, obtaining high-purity CO 2 And (3) gas.
It should be noted that the structure of the lime kiln is not limited in this application, and for example, the lime kiln may be a conventional dual-chamber lime shaft kiln structure. The kiln mainly comprises two kiln bores which are mirror images of each other, and a connecting channel for communicating gas is arranged between the two kiln bores. One of the two kiln chambers is a combustion chamber, comprises a calcination section positioned at the upper part and a cooling section positioned at the lower part, and the other kiln chamber is a heat storage chamber, namely a preheating section of the lime kiln. The two kiln bores periodically exchange roles, thereby completing the continuous calcination of lime.
As a preferred scheme, the oxygen conveying pipeline is connected to the heat exchanger firstly, and the hot oxygen pipeline led out from the outlet of the heat exchanger and the combustion-supporting flue gas pipeline are connected to the combustion-supporting air pipeline after being combined, namely cold or normal-temperature oxygen conveyed by the oxygen conveying pipeline exchanges heat with flue gas discharged into the heat exchanging pipeline from the preheating section in the heat exchanger, and then enters the combustion-supporting air pipeline to heat up, and the cold or normal-temperature oxygen enters the combustion-supporting air pipeline and CO in the combustion-supporting flue gas pipeline 2 The two gases are mixed in the combustion-supporting air pipeline to form combustion-supporting air with a certain temperature, and then the combustion-supporting air is sent to the calcining section, so that the combustion-supporting effect can be improved, the fuel consumption is reduced, and the production efficiency is improved. For strengthening the mixing effect of combustion-supporting wind, this application adds the blender in the position that hot oxygen pipeline and combustion-supporting flue gas pipeline both merge, the export and the combustion-supporting tuber pipe of blender are connected.
Further preferably, the utility model will draw low temperature from another outlet of the heat exchangerThe hot air pipeline is divided into two branches, namely a cooling air pipeline and CO 2 And (5) a finished pipeline. Wherein the cooling air duct is connected to the cooling air inlet of the cooling section. CO 2 The finished pipeline is connected to CO 2 A finished product system. That is, the combustion air of the calcining section is changed from the common air combustion air into oxygen and CO 2 On the basis of oxygen-enriched combustion-supporting air formed by mixing gas, the cooling medium of the cooling section is changed into CO from common air 2 The main component of the high-temperature flue gas generated by the air flow, the calcining section and the cooling section is CO 2 Gases, i.e. avoiding the introduction of oxygen and N during fuel combustion and air-based cooling of the prior art 2 CO of the impurity components 2 Is diluted to realize CO 2 Enrichment of gas greatly improves CO in tail gas of lime production 2 Concentration. Thus, the high-temperature flue gas (namely high-purity CO) generated by the calcining section and the cooling section can be recycled by the flue gas 2 Gas) is respectively used for fuel transportation, mixing of combustion-supporting air, cooling gas and high-purity CO after preheating limestone materials 2 And (5) producing a finished product. And CO after heat exchange and temperature reduction with oxygen in the heat exchanger 2 The gas is then conveyed to a cooling section or is output as a product, and CO required by each process in the system is realized 2 The self-circulation supply of the gas maximizes the waste heat utilization of the flue gas and ensures the effect of each working procedure.
The utility model also provides a cooler on the cooling air pipeline for exchanging heat with oxygen and cooling down CO 2 The gas is conveyed to a cooling section after being cooled down, so that the cooling effect on the high-temperature CaO generated by calcination is enhanced, and the cooling of the obtained finished lime is ensured to be complete. The cooler is not limited, and may be, for example, a water bath or an air cooler.
Generally, CO 2 The utility model breaks the routine, changes the traditional air combustion-supporting wind into oxygen and CO in the calcining section 2 Oxygen-enriched combustion-supporting wind formed by mixing the gases. First, the air combustion air is replaced by oxygen and CO 2 Combustion-supporting air of the mixed gas can avoid N in the air 2 CO of the impurity components 2 The product after combustion of the fuel is mainly CO 2 Further improving CO in the flue gas generated in the calcination process 2 Is a concentration of (2); second, oxygen and CO 2 The combustion-supporting air of the mixed gas is compared with the air combustion-supporting air, and the inert components of the mixed gas and the air combustion-supporting air are CO respectively 2 And N 2 And CO 2 And N 2 Different in thermal physical properties, CO 2 Has a specific heat capacity of about 840j/kg-K, N 2 The specific heat capacity of (C) is about 740j/kg-K, so that the oxygen and CO in the scheme of the application 2 The combustion-supporting air of the mixed gas can better meet the heat transfer in the lime production system, and the production efficiency is improved. In addition, if the combustion-supporting air adopts pure oxygen, oxygen is likely to be unreacted completely, namely, the impurity components such as introduced oxygen and the like are introduced into CO in the fuel combustion process 2 Dilution conditions; likewise, CO 2 Different from oxygen in thermal properties, CO 2 The specific heat capacity of the catalyst is obviously larger than that of oxygen, namely CO is introduced into combustion air 2 The components can ensure the heat transfer of the system and greatly improve the CO in the tail gas in the lime production process 2 Concentration, realizes the production of lime and simultaneously, CO 2 The recycling of the gas effectively overcomes the problem of CO in the existing lime production process 2 Large discharge and resource waste.
In the present application, in view of the control of the combustion temperature, in the spatial combustion of porous media such as lime kiln, in order to maintain a combustion temperature similar to that of air combustion, a suitable combustion atmosphere is maintained, in which oxygen and CO 2 In the combustion-supporting air formed by mixing the gases, the concentration (volume ratio) of oxygen is generally maintained at 27-31%, and CO 2 The volume ratio of (3) is 69-73%. Wherein the specific concentration value is related to the fuel type and heating value. For example, when using a typical fuel blast furnace gas on a lime kiln, the concentration of oxygen is about 27-28%. In order to ensure the ratio of two gases in the mixed combustion-supporting air and maintain proper combustion atmosphere, the utility model is provided with a first valve on the combustion-supporting flue gas pipeline, and a second valve on the oxygen conveying pipeline (or hot oxygen pipeline), wherein the two valves are used for controlling oxygen and CO in the combustion-supporting air 2 The amount of gas is regulated and controlled in real time as required.
The utility model arranges a first diverter at the position of the flue gas exhaust pipeline for separating the fuel air delivery pipeline, the combustion-supporting flue gas pipeline and the heat exchange pipeline, and separates the cooling air pipeline and the CO at the low-temperature hot air pipeline 2 The second flow dividers are arranged at the positions of the two branches of the finished product pipeline, and the arrangement of the two flow dividers can realize the real-time on-demand regulation and control of the distribution proportion of the exhaust smoke of the preheating section.
In the application, the tail gas CO is produced by adopting the lifting lime 2 The main process of the lime production system for lime production comprises 3 main working procedures of preheating, calcining, cooling and the like, which are used for material flow, and 7 auxiliary working procedures of primary mixing, dust removal, primary split flow, heat exchange, secondary mixing, secondary split flow, water bath (or cooling) and the like, which are used for material flow, are used for assisting. The method comprises the following steps:
main process (stream process):
preheating: high temperature air (about 850 ℃) is obtained by adopting the calcination and cooling procedures to uniformly heat the massive limestone material to about 600 ℃. Calcining: the limestone is quickly heated to the calcining temperature (1050 ℃) by using high-temperature flue gas generated by burning solid fuels such as raw coal, so as to lead CaCO (CaCO) 3 Rapidly complete decomposition, produce CaO and release CO 2 . And (3) cooling: the high temperature lump CaO obtained by calcination uses CO at about 20 DEG C 2 And cooling the air flow to below 100 ℃ to obtain blocky finished lime, and feeding the blocky finished lime into a lime finished product system.
Auxiliary step (gas flow step):
primary mixing: two high temperature CO generated in the calcination step and the cooling step 2 The gases (the temperature is 1050 ℃ and about 600 ℃ respectively) are uniformly mixed, the temperature of the mixed gases is about 850 ℃, and the mixed high-temperature flue gas is used for preheating normal-temperature limestone (about 20 ℃). Dedusting: the temperature of the high-temperature flue gas after the preheating procedure is reduced from 850 ℃ to about 120 ℃, and a large amount of CaCO is mixed in the flue gas 3 And CaO dust, and removing the dust in the flue gas by electric dust removal or cloth bag dust removal before entering a downstream process. Primary shunt: the flue gas after dust removal and purification (the main component is CO) 2 Gas) is split into three streams,respectively used for downstream pulverized coal conveying, oxygen preheating and combustion-supporting air mixing, namely a part of CO 2 The gas is used as carrier gas for pulverized coal conveying, and a part of CO 2 The gas is sent to a downstream heat exchange process, preheated to be used as combustion-supporting pure oxygen and the residual CO 2 The gas is used as combustion-supporting air component and preheated O 2 Mixing (i.e., secondary mixing process). Heat exchange: the heat exchange is carried out on the industrial pure oxygen (about 20 ℃ at normal temperature) and the smoke after primary diversion, the temperature of the oxygen is raised to about 100 ℃, and the temperature of the smoke is further reduced to about 80 ℃. Secondary split: splitting the flue gas into two streams, one stream being fed to a downstream water bath process and the other stream being high purity CO 2 The product is directly produced and sent into CO 2 A finished product system. And (3) water bath: after the secondary split flue gas passes through the water bath, the temperature is further reduced to about 20 ℃, and then the flue gas is used as cooling gas to be conveyed to a cooling process.
Compared with the prior art, the utility model has the following beneficial effects:
1. the utility model changes the common air combustion-supporting air of the calcining section into oxygen and CO 2 Oxygen-enriched combustion-supporting air formed by mixing gases, and changing cooling medium of cooling section from common air into CO 2 Air flow, thereby avoiding N in the prior art 2 CO of the impurity components 2 Greatly improves the tail gas CO in the lime production process 2 Concentration, i.e. high purity CO can be obtained while lime is being produced 2 Gaseous byproducts.
2. The utility model uses two high temperature CO generated by the calcining section and the cooling section 2 The mixed gas is split for downstream cooling gas, coal powder conveying and combustion-supporting air preheating and mixing and high-purity CO 2 Yield of finished product by CO 2 The enrichment and circulation of the gas can realize the CO required by the working procedures of cooling the gas, transporting the carrier gas by the fuel, preheating and mixing the combustion-supporting air and the like in the system 2 Self-circulation supply of gas while obtaining high purity CO 2 Gas, i.e. CO 2 The gas is recycled, thereby avoiding the CO in the existing lime production process 2 Large discharge and resource waste.
3. The present utility model breaks the conventional manner and,by oxygen and CO 2 Combustion-supporting air of mixed gas, avoiding N in the prior art 2 Or O 2 CO of the impurity components 2 And (2) dilution of CO 2 Has a specific heat capacity greater than N 2 And O 2 Specific heat capacity of (2), i.e. introducing CO into combustion air 2 The components can ensure the heat transfer of the system and greatly improve the CO in the tail gas in the lime production process 2 Concentration, realizes the production of lime and simultaneously, CO 2 And recycling the gas.
Drawings
FIG. 1 shows a method for improving CO in tail gas of lime production 2 A structural schematic diagram of a concentrated lime production system;
FIG. 2 is a flow chart of a prior art lime production process.
Reference numerals:
a: lime kiln; a1: a preheating section; a2: a calcination section; a3: a cooling section; 1: a heat exchanger; 2: CO 2 A finished product system; 3: a cooler; 4: a mixer; 501: a first shunt; 502: a second splitter; 6: a dust remover; 701: a first valve; 702: a second valve; 8: a lime finished product system;
l1: a combustion air duct; l2: a flue gas discharge duct; l3: a fuel air supply pipeline; l4: a combustion-supporting flue gas pipeline; l5: a heat exchange pipeline; l6: an oxygen delivery conduit; l7: a hot oxygen pipe; l8: a low temperature hot air duct; l9: a cooling air duct; l10: CO 2 And (5) a finished pipeline.
Detailed Description
The following examples illustrate the technical aspects of the utility model, and the scope of the utility model claimed includes but is not limited to the following examples.
According to an embodiment of the utility model, a method for improving CO in tail gas of lime production is provided 2 A lime production system of concentration.
Promote lime production tail gas CO 2 A concentrated lime production system comprising a lime kiln a. A preheating section A1, a calcining section A2 and a cooling section A3 are arranged in the lime kiln A. A fuel spray gun is arranged in the calcining section A2, and the calcining section A2 is connected with a combustion air pipeline L1.The flue gas outlets of the calcining section A2 and the cooling section A3 are connected to the preheating section A1. The smoke exhaust pipeline L2 led out from the smoke outlet of the preheating section A1 is divided into three branches, namely a fuel air conveying pipeline L3, a combustion-supporting smoke pipeline L4 and a heat exchange pipeline L5. Wherein the fuel supply air duct L3 is connected to the fuel spray gun. The combustion-supporting flue gas pipeline L4 is connected to a combustion-supporting air pipeline L1, and an oxygen conveying pipeline L6 is connected to the combustion-supporting air pipeline L1 at the same time. The heat exchange pipe L5 is connected to the heat exchanger 1.
Preferably, the oxygen delivery pipe L6 is connected to the heat exchanger 1, and the hot oxygen pipe L7 and the combustion-supporting flue gas pipe L4 led out from the outlet of the heat exchanger 1 are connected to the combustion-supporting air pipe L1 after being combined.
In the utility model, a low-temperature hot air pipeline L8 led out from the other outlet of the heat exchanger 1 is divided into two branches, namely a cooling air pipeline L9 and a CO respectively 2 And a finished pipeline L10. Wherein the cooling air duct L9 is connected to the cooling air inlet of the cooling section A3. CO 2 The finished pipeline L10 is connected to CO 2 The finished system 2.
Preferably, the cooling air duct L9 is further provided with a cooler 3. Preferably, the cooler 3 is a water bath or an air cooler.
Preferably, the system further comprises a mixer 4. The mixer 4 is arranged at a position where the hot oxygen pipeline L7 and the combustion-supporting flue gas pipeline L4 are combined. The outlet of the mixer 4 is connected with a combustion air pipeline L1.
In the present utility model, the system further comprises a first shunt 501. The first diverter 501 is arranged at the position of the three branches of the flue gas discharge pipeline L2, namely the fuel delivery and air supply pipeline L3, the combustion-supporting flue gas pipeline L4 and the heat exchange pipeline L5.
In the present utility model, the system further comprises a second diverter 502. The second splitter 502 is arranged on the low-temperature hot air pipeline L8 to split cooling air pipelines L9 and CO 2 The positions of the two branches of the finished pipeline L10.
In the present utility model, the system further comprises a dust remover 6. The dust remover 6 is arranged on the fume exhaust pipeline L2. Preferably, the dust remover 6 is an electric dust remover or a cloth bag dust remover.
In the present utility model, the first valve 701 is provided on the combustion-supporting flue gas duct L4. The oxygen transmission pipeline L6 or the hot oxygen pipeline L7 is provided with a second valve 702.
In the present utility model, the system also includes a lime finishing system 8. The discharge port arranged at the bottom of the cooling section A3 of the lime kiln A is connected with a lime finished product system 8.
Example 1
As shown in fig. 1, a method for improving CO in tail gas of lime production 2 A concentrated lime production system comprising a lime kiln a. A preheating section A1, a calcining section A2 and a cooling section A3 are arranged in the lime kiln A. A fuel spray gun is arranged in the calcining section A2, and the calcining section A2 is connected with a combustion air pipeline L1. The flue gas outlets of the calcining section A2 and the cooling section A3 are connected to the preheating section A1. The smoke exhaust pipeline L2 led out from the smoke outlet of the preheating section A1 is divided into three branches, namely a fuel air conveying pipeline L3, a combustion-supporting smoke pipeline L4 and a heat exchange pipeline L5. Wherein the fuel supply air duct L3 is connected to the fuel spray gun. The combustion-supporting flue gas pipeline L4 is connected to a combustion-supporting air pipeline L1, and an oxygen conveying pipeline L6 is connected to the combustion-supporting air pipeline L1 at the same time. The heat exchange pipe L5 is connected to the heat exchanger 1.
In this embodiment, the lime kiln a is a dual-chamber lime shaft kiln, which mainly comprises two kiln chambers that are mirror images of each other, and a connecting channel that is formed between the two kiln chambers and is used for communicating gas is provided. One of the two kiln chambers is a combustion chamber, comprises a calcination section positioned at the upper part and a cooling section positioned at the lower part, and the other kiln chamber is a heat storage chamber, namely a preheating section of the lime kiln. The two kiln bores periodically exchange roles, thereby completing the continuous calcination of lime.
Example 2
Example 1 was repeated except that the oxygen-carrying line L6 was connected to the heat exchanger 1 first, and both the hot oxygen line L7 and the combustion-supporting flue gas line L4, which were led out from the outlet of the heat exchanger 1, were connected to the combustion-supporting air line L1 after being combined.
Example 3
Example 2 was repeated except that the low-temperature hot air duct L8 led out from the other outlet of the heat exchanger 1 was branched into two branches, namely, a cooling air duct L9 and CO 2 And a finished pipeline L10.Wherein the cooling air duct L9 is connected to the cooling air inlet of the cooling section A3. CO 2 The finished pipeline L10 is connected to CO 2 The finished system 2.
Example 4
Example 3 was repeated except that the cooling air duct L9 was further provided with a cooler 3. The cooler 3 is a water bath.
Example 5
Example 3 was repeated except that the cooling air duct L9 was further provided with a cooler 3. The cooler 3 is an air cooler.
Example 6
Example 4 is repeated except that the system further comprises a mixer 4. The mixer 4 is arranged at a position where the hot oxygen pipeline L7 and the combustion-supporting flue gas pipeline L4 are combined. The outlet of the mixer 4 is connected with a combustion air pipeline L1.
Example 7
Example 6 is repeated except that the system further comprises a first shunt 501. The first diverter 501 is arranged at the position of the three branches of the flue gas discharge pipeline L2, namely the fuel delivery and air supply pipeline L3, the combustion-supporting flue gas pipeline L4 and the heat exchange pipeline L5.
Example 8
Example 7 is repeated except that the system further comprises a second diverter 502. The second splitter 502 is arranged on the low-temperature hot air pipeline L8 to split cooling air pipelines L9 and CO 2 The positions of the two branches of the finished pipeline L10.
Example 9
Example 8 is repeated except that the system further comprises a dust separator 6. The dust remover 6 is arranged on the fume exhaust pipeline L2. The dust remover 6 is an electric dust remover.
Example 10
Example 8 is repeated except that the system further comprises a dust separator 6. The dust remover 6 is arranged on the fume exhaust pipeline L2. The dust remover 6 is a cloth bag dust remover.
Example 11
Embodiment 10 is repeated except that the combustion flue gas duct L4 is provided with a first valve 701. A second valve 702 is provided on the hot oxygen line L7.
Example 12
Example 11 is repeated except that the system also includes a lime finishing system 8. The discharge port arranged at the bottom of the cooling section A3 of the lime kiln A is connected with a lime finished product system 8.
Claims (25)
1. Promote lime production tail gas CO 2 A lime production system of concentration, the system comprising a lime kiln (a); a preheating section (A1), a calcining section (A2) and a cooling section (A3) are arranged in the lime kiln (A); a fuel spray gun is arranged in the calcining section (A2), and the calcining section (A2) is connected with a combustion-supporting air pipeline (L1); the flue gas outlets of the calcining section (A2) and the cooling section (A3) are connected to the preheating section (A1); the smoke exhaust pipeline (L2) led out from the smoke outlet of the preheating section (A1) is divided into three branches, namely a fuel air conveying pipeline (L3), a combustion-supporting smoke pipeline (L4) and a heat exchange pipeline (L5); wherein the fuel supply air duct (L3) is connected to the fuel lance; the combustion-supporting flue gas pipeline (L4) is connected to the combustion-supporting air pipeline (L1), and the combustion-supporting air pipeline (L1) is simultaneously connected with an oxygen conveying pipeline (L6); the heat exchange pipeline (L5) is connected to the heat exchanger (1).
2. The lime production system of claim 1, wherein: the oxygen conveying pipeline (L6) is connected to the heat exchanger (1) firstly, and the hot oxygen pipeline (L7) and the combustion-supporting flue gas pipeline (L4) led out from the outlet of the heat exchanger (1) are connected to the combustion-supporting air pipeline (L1) after being combined.
3. The lime production system of claim 2, wherein: the low-temperature hot air pipeline (L8) led out from the other outlet of the heat exchanger (1) is divided into two branches, namely a cooling air pipeline (L9) and CO 2 A finished pipe (L10); wherein the cooling air duct (L9) is connected to the cooling air inlet of the cooling section (A3); CO 2 The finished pipeline (L10) is connected to CO 2 A finished product system (2).
4. A lime production system according to claim 3, wherein: the cooling air pipeline (L9) is also provided with a cooler (3).
5. The lime production system of claim 4, wherein: the cooler (3) is a water bath or an air cooler.
6. A lime production system according to any one of claims 2-5, wherein: the system further comprises a mixer (4); the mixer (4) is arranged at a position where the hot oxygen pipeline (L7) and the combustion-supporting flue gas pipeline (L4) are combined; the outlet of the mixer (4) is connected with a combustion-supporting air pipeline (L1).
7. A lime production system according to any one of claims 1-5, wherein: the system further comprises a first shunt (501); the first flow divider (501) is arranged at the position of a smoke exhaust pipeline (L2) for separating three branches of a fuel air conveying pipeline (L3), a combustion-supporting smoke pipeline (L4) and a heat exchange pipeline (L5).
8. The lime production system of claim 6, wherein: the system further comprises a first shunt (501); the first flow divider (501) is arranged at the position of a smoke exhaust pipeline (L2) for separating three branches of a fuel air conveying pipeline (L3), a combustion-supporting smoke pipeline (L4) and a heat exchange pipeline (L5).
9. A lime production system according to any one of claims 3-5, wherein: the system further includes a second shunt (502); the second flow divider (502) is arranged on the low-temperature hot air pipeline (L8) to divide the cooling air pipeline (L9) and the CO 2 The positions of the two branches of the finished pipeline (L10).
10. The lime production system according to any one of claims 1-5, 8, wherein: the system also comprises a dust remover (6); the dust remover (6) is arranged on the flue gas discharge pipeline (L2).
11. The lime production system of claim 6, wherein: the system also comprises a dust remover (6); the dust remover (6) is arranged on the flue gas discharge pipeline (L2).
12. The lime production system of claim 7, wherein: the system also comprises a dust remover (6); the dust remover (6) is arranged on the flue gas discharge pipeline (L2).
13. The lime production system of claim 9, wherein: the system also comprises a dust remover (6); the dust remover (6) is arranged on the flue gas discharge pipeline (L2).
14. The lime production system of claim 10, wherein: the dust remover (6) is an electric dust remover or a cloth bag dust remover.
15. A lime production system according to any one of claims 11-13, wherein: the dust remover (6) is an electric dust remover or a cloth bag dust remover.
16. The lime production system of any one of claims 2-5, 8, 11, 13, wherein: a first valve (701) is arranged on the combustion-supporting flue gas pipeline (L4); the oxygen transmission pipeline (L6) or the hot oxygen pipeline (L7) is provided with a second valve (702).
17. The lime production system of claim 6, wherein: a first valve (701) is arranged on the combustion-supporting flue gas pipeline (L4); the oxygen transmission pipeline (L6) or the hot oxygen pipeline (L7) is provided with a second valve (702).
18. The lime production system of claim 9, wherein: a first valve (701) is arranged on the combustion-supporting flue gas pipeline (L4); the oxygen transmission pipeline (L6) or the hot oxygen pipeline (L7) is provided with a second valve (702).
19. The lime production system of any one of claims 1-5, 8, 11-14, 17-18, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
20. The lime production system of claim 6, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
21. The lime production system of claim 7, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
22. The lime production system of claim 9, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
23. The lime production system of claim 10, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
24. The lime production system of claim 15, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
25. The lime production system of claim 16, wherein: the system also comprises a lime finishing system (8); the discharge opening arranged at the bottom of the cooling section (A3) of the lime kiln (A) is connected with a lime finished product system (8).
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